Ionic liquid catalyst for improvement of heavy and extra heavy crude

Abstract

The present invention relates to improving heavy crude oil, and extra through a scheme considering the use of ionic liquids catalysts based on Mo and Fe catalyst is highly miscible with crude oil and are in the homogeneous phase crude oil. Furthermore, this invention relates to improving heavy crude in two stages, the first ionic liquid catalyst, and the second supported catalyst. The API gravity crude is increased from 12.5 to 19 points in the first stage and viscosities up to 5600-1600 decreased from 60-40 cSt certain to 37.8° C. While in the second stage, you get an upgraded crude oil with 32.9° API, viscosity of 4.0 cSt, reduction in total sulphur content of 0.85 wt % nitrogen and 0295 ppm by weight, respectively. As a considerable reduction of asphaltenes from 28.65 to 3.7% weight.

The invention claimed is: 
     
       1. An ionic liquid catalyst for processing heavy and extra heavy crude oil, wherein said ionic liquid catalyst includes an inorganic salt comprising a Group VIII metal, in the range of 0.3 to 0.7% by weight, and inorganic salts of a Group VIA metal in a range of 0.1 to 0.5% by weight in an aqueous base and where said Group VIA metal is a phosphomolybdate present in the form of a heteropolyacid and has the formula (PMo 12 O 40 ) −3 . 
     
     
       2. An ionic liquid catalyst for processing heavy and extra heavy crude oil, wherein said ionic liquid catalyst includes ferric sulphate in an amount of 0.3 to 0.7% by weight, and a Group VIA metal salt in an amount of 0.1 to 0.5% by weight in an aqueous base. 
     
     
       3. An ionic liquid catalyst in accordance with  claim 1 , wherein the inorganic salt of the Group VIA metal is ammonium molybdate, and where said ionic liquid catalyst is activated in a hydrogen atmosphere at a temperature of 200° C. to 350° C. 
     
     
       4. A method of processing heavy and extra heavy crude oil, which consists of: a) adding to an oil field (in situ) the ionic liquid catalyst of  claim 2  in concentrations of 0.5 to 10% weight, b) mixing homogeneously; c) pressurized with hydrogen to less than 50 kg/cm 2 , d) increase temperature to 250 to 420° C. and pressure 50 to 125 Kg/cm 2 , for a residence time of reaction 2 to 20 hours for the disintegration of resins and asphaltenes to lower molecular weight hydrocarbons. 
     
     
       5. The method in accordance with  claim 4 , where the active elements based on Mo, and Fe, are activated in situ at temperatures of 225-275° C. 
     
     
       6. The method in accordance with  claim 4 , in which the heavy and extra heavy crude oils have API gravity of 4 to 14 degrees and viscosity up to 60,000 cSt @ 25° C. 
     
     
       7. The method in accordance with  claim 4 , wherein said heavy and extra heavy crude oil increases in API gravity of at least 4 units and up to 10 units and decreases the viscosity of the oil processed to 40 cSt @ 25° C. 
     
     
       8. The method in accordance with  claim 4 , which increases a distillable fraction of heavy and extra heavy crude oils processed in an amount of at least 18% wt. 
     
     
       9. The method in accordance with  claim 4 , where the heavy and extra heavy crude oils treated decrease the concentration of asphaltenes contained up to 50% and eliminated 30 to 40% of the sulphur content. 
     
     
       10. A method of processing heavy and extra heavy crude oil using the ionic liquid catalyst in accordance with  claim 2 , wherein a first stage consists of: a) the ionic liquid catalyst and crude oil are pre-mixed and homogenized in feed pump at a temperature between 200-300° C., before entering a reactor packed with a static switch that contains several elements so mixed assemblies that are between them at an angle of 90°, b) immediately, crude oil and ionic liquid catalyst pre-activated homogenized and mixed with a stream of hydrogen in the temperature range between 350-450° C., so that reactions occur hydrocracking/hydrogenation of asphaltenes and resins at 250-420° C. and pressures from 50 to 125 Kg/cm 2  for a residence time of reaction 2 to 20 hours, a second step: c) mixing the reaction products of the first phase with a stream of hydrogen to feed a fixed bed reactor packed with a catalyst NiCoMoWP based multimetallic supported on alumina and/or in silico-aluminate, amorphous or crystalline, in concentrations from 5 to 15% by weight a temperature between 250-420° C. and pressures between 50 and 125 Kg/cm 2  with a residence time of 2 to 30 hours, taking place hydrocracking reactions, hydrodesulfurization and hydrogenation of aromatics, conversion of resins and asphaltenes to lower molecular weight structures. 
     
     
       11. The method in accordance with  claim 10 , wherein the API gravity crude is increased from 12.5 to 19 points in the first stage and the viscosity decreases from 5600-1600 to 60-40 cSt certain @ 37.8° C., while in the second stage, a crude oil is obtained with API gravity of 32.9°, viscosity of 4.0 cSt, reduction in total sulfur content of 0.85 wt % nitrogen and 295 ppm by weight, respectively, and asphaltenes reduction of 28.65 to 3.7% by weight. 
     
     
       12. The catalyst of  claim 1 , wherein said catalyst comprises iron and molybdenum. 
     
     
       13. The ionic liquid catalyst of  claim 1 , wherein said Group VIII metal is ferric sulfate. 
     
     
       14. The ionic liquid catalyst of  claim 2 , wherein said Group VIA metal salt is a phosphomolybdate having the formula (PMo 12 O 40 ) −3 . 
     
     
       15. The method of  claim 4 , wherein said ionic liquid catalyst is present in an amount of 2.0 to 0.1 wt % based on the weight of the crude oil. 
     
     
       16. An ionic liquid catalyst for processing heavy and extra heavy crude oil, wherein said ionic liquid catalyst comprises a Group VIII metal inorganic salt and phosphomolybdate having the formula (PMo 12 O 40 ) −3 . 
     
     
       17. The ionic liquid catalyst of  claim 16 , wherein said Group VIII metal inorganic salt is present in an amount of 0.3 to 0.7% by weight, and said phosphomolybdate is present in an amount of 0.1 to 0.5% by weight in an aqueous base. 
     
     
       18. An ionic liquid catalyst for processing heavy and extra heavy crude oil, wherein said ionic liquid catalyst comprises a Group VIII metal inorganic salt and a phosphomolybdate, wherein said Group VIII metal is iron. 
     
     
       19. The ionic liquid catalyst of  claim 16 , wherein said Group VIII metal is ferric sulfate. 
     
     
       20. A method of processing heavy and extra heavy crude oil, comprising the steps of:
 admixing an ionic liquid catalyst and crude oil at concentration of 0.5 to 10% by weight to obtain a mixture, wherein said ionic liquid catalyst comprises a molybdenum salt and an iron salt in the form of a heteropoly acid, wherein said Group VIII metal salt is ferric sulfate, and 
 heating the resulting mixture to a temperature of 250° to 420° C. and pressure 50 to 125 Kg/cm 2  in the presence of hydrogen, for a time sufficient for the disintegration of resins and asphaltenes to lower molecular weight hydrocarbons. 
 
     
     
       21. The method of  claim 20 , wherein said crude oil has an API gravity of 4 to 14 degrees. 
     
     
       22. The method of  claim 20 , wherein said molybdenum is present in the form of phosphomolybdate having the formula (PMo 12 O 40 ) −3 . 
     
     
       23. The method of  claim 20 , further comprising activating said ionic liquid catalyst by pressurizing said ionic liquid catalyst with hydrogen to a pressure less than 50 kg/cm 2  and heating to a temperature of 200° to 350° C.